Inlet distributor for downflow reactor

ABSTRACT

An inlet distributor for a gas solids contracting vessel uses a two direction distributor to prevent bed surface disturbances at high inlet velocities and high particle loadings. The distributor uses a series of partitions to peel off portions of the downward gas flow and redirect them radially outward. Each outwardly directed gas flow component passes through a series of perforations to effect any necessary circumferential redistribution before entering the space above the particle bed. By subdividing the gas flow into a number of radially directed flow portions and circumferentially redistributing these flow portions, cross-currents and eddy currents on the catalyst bed surface are minimized or avoided so that disturbances at the bed surface are eliminated. This distributor is particularly effective in vessels having particles loaded to within a short distance of bed inlets and where elbows or other upstream flow devices introduce nonuniformities into the gas flow to a particle bed. The distributor has a simple arrangement and can be used without adding significant pressure drop to the system.

BACKGROUND OF THE INVENTION

This invention relates generally to the field of fluid-solid contacting.More specifically, this invention deals with the delivery of fluids tobeds of particulate material.

Fluid-solid contacting devices have a wide variety of applications. Suchdevices find common application in processes for hydrocarbon conversionand adsorption columns for separation of fluid components. When thefluid-solid contacting device is an adsorption column, the particulatematerial will comprise an adsorbent through which the fluid passes. Inthe case of hydrocarbon conversion, the fluid-solid contacting apparatusis typically a reactor containing catalyst. Typical hydrocarbonconversion reactions that may be carried out are hydrogenation,hydrotreating, hydrocracking, and hydrodealkylation.

Fluid-solid contacting devices to which this invention apply arearranged as an elongated cylinder usually having a vertical orientationthrough which an essentially vertical flow of fluid is maintained.Particulate material contained in this vessel is arranged in one or morebeds. Fluid enters the vessel through an inlet located at an upstreamend of the vessel. It is also commonly known to add or withdraw fluidfrom between the particulate beds. This is commonly done in adsorptionschemes where the composition of the fluid passing between particle bedsis changing or in hydrocarbon conversion processes where a quench systemis used to cool fluid as it passes between beds.

Changes in the composition or properties of the fluid passing throughthe particular zone present little problem provided these changes occuruniformly. In adsorption systems these changes are the result ofretention or displacement of fluids within the adsorbent. For reactionsystems changes in temperature as well as composition of the fluid arecaused by the particulate catalyst material contained in the beds.

Nonuniform flow of fluid through these beds can be caused by poorinitial mixing of the fluid entering the bed or variations in flowresistance across the particulate bed. Variations in the flow resistanceacross the bed can vary contact time of the fluid within the particlesthereby resulting in uneven reactions or adsorption of the fluid streampassing through the bed. In extreme instances, this is referred to aschanneling wherein fluid over a limited portion of the bed is allowed tomove in a narrow open area with virtually no resistance to flow. Whenchanneling occurs, a portion of the fluid passing through the bed willhave minimal contact with the particulate matter of the bed. If theprocess is one of adsorption, the fluid passing through the channel areawill not be absorbed, thereby altering the composition of this fluidwith respect to fluid passing through other portions of the absorbentbed. For a catalytic reaction, the reduction in catalyst contact timewill also alter the product composition of fluid as it leaves differentportions of the catalyst bed.

In addition to problems of fluid composition, irregularities in theparticulate bed can also affect the density and temperature of the fluidpassing through the bed. For many separation processes retained anddisplaced components of the fluid have different densities which tend todisrupt the flow profile through the bed. Nonuniform contacting with theadsorbent particles will exacerbate the problem by introducing morevariation in the density of the fluid across the bed thereby furtherdisrupting the flow profile of the fluid as it passes through theparticle bed.

In reaction zones, temperature variations are most often associated withnonuniform catalyst contact due to the endothermic or exothermic natureof such systems. Nonuniform contact with the catalyst will adverselyaffect the reaction taking place by overheating or overcooling thereactants. This problem is most severe in exothermic reactions where thehigher temperature can cause further reaction of feedstock or otherfluid components into undesirable products or can introduce local hotspots that will cause damage to the catalyst and/or mechanicalcomponents.

Fluid flow into the vessel can disrupt the top surface of the bed. Thedisruption results from transverse fluid flow across the surface of thebed at velocities sufficient to move the individual bed particles. For aconfined bed, this disruption or movement of the particles will causethe particles to abrade against each other generating smaller particleswhich are referred to as fines. These fines may increase pressure dropwithin the bed or escape from the bed thereby reducing the overallquantity of particles in the bed and possibly interfering withdownstream operations. In unconfined beds, transverse fluid flow mayalso shift large quantities of particles so that the bed surface ishighly irregular.

These transverse currents are the result of charging fluid into arelatively large diameter vessel through a relatively small diameternozzle. Charging fluid into the vessel through a small diameter nozzleproduces a high velocity jet that extends from the nozzle into thevessel. Impact of this jet on or adjacent to the surface of a relativelyclosed catalyst bed flares the fluid outward thereby producing eddycurrents and fluid velocities transverse to the bed surface. The inleteffects associated with the relatively small diameter nozzle arecompounded by the usual presence of an elbow just upstream of the nozzlewhich introduces another transverse velocity component into the fluidflow entering the vessel. The overall result of these inlet effects isoften the piling up of particles around the periphery of the particlebed or the shifting of particles from one side of the bed to the other.

These detrimental inlet effects are avoided by uniformly dispersing thefluid as it enters the vessel. Uniform dispersal can be obtained byproviding a sufficient length between the nozzle and the catalyst bedsurface such that the fluid jet and any transverse velocities aresubstantially dissipated upstream of the particle bed. However, in mostcases, it is impractical to provide the length necessary for dissipationof the inlet effects due to the excessive vessel tangent length thatwould be required. In fact, the trend in many industries is to decreasethe length between the inlet nozzle and the particle bed surface inorder to increase the total volume of particles in the vessel andthereby obtain greater fluid throughput or greater particle bed servicelife.

For these reasons, inlet distributors are commonly used to break up thefluid jet and redistribute fluid flow over the top surface of a particlebed. One such device is shown in U.S. Pat. No. 2,925,331 issued toKazmierczak et al. where a fluid stream is downwardly directed onto theupper surface of the catalyst bed and passes first through a distributorconsisting of a series of annular plates having inner diameters thatprogressively decrease in the direction of fluid flow so that portionsof the fluid stream are in effect peeled off and redirected radiallyoutward over the surface of the particle bed. It is also known in thehydrocarbon processing industry to attach cylindrical rings extending inthe direction of fluid flow to the inner edge of the annular plates.Another type of distributor used to redirect and remix fluid flowupstream of a particle bed is shown in U.S. Pat. No. 3,598,541 issued toHennemuth et al. and U.S. Pat. No. 3,598,542 issued to Carson et al. TheHennemuth distributor uses a series of circumferentially spaced holes toredistribute fluid within a fluid mixing device that communicates withthe upper surface of a particle bed. The distributor disclosed in Carsonuses a series of circumferentially spaced holes to radially dischargefluid across the upper surface of a particle bed. Thus, the prior art iswell acquainted with a number of distribution devices for use in fluidsolid contacting vessels.

Despite the use of different inlet distributors, bed disruption remainsa problem. Distributors that use the annular plates or baffles of theKazmierczak device reduce the severity of bed disturbances but have noteliminated it. Therefore, large scale shifting of particle bed surfaces,especially where fluid inlet velocities are high, still occurs. Suchdisruption is still known to occur even in cases where straighteningvanes and other flow distribution devices are added to the upstreamelbow as a means of eliminating a resulting transverse flow component.It has now been discovered that despite the presence of the baffles andadditional redistribution devices, such as straightening vanes, fluidflow entering the vessel still remembers the change of direction thattook place upstream of the inlet nozzle.

SUMMARY OF THE INVENTION

Therefore, it is an object of this invention to improve fluid dispersalover the surface of a particulate bed.

It is a further object of this invention to prevent disruption of thetop surface of the bed.

It is a yet further objective of this invention to dissipate inleteffects such as jets and transverse currents associated with fluid flowinto a vessel while minimizing the distance between the inlet nozzle andthe particle bed surface.

Another object of this invention is to provide a fluid distributor thateliminates transverse velocity components that enter the vessel througha relatively small nozzle.

These and other objects are satisfied by the device of this inventionwhich is the first inlet distributor to radially and circumferentiallyredirect a majority of an axial fluid flow over the surface of aparticle bed. This redistribution dissipates nonuniform transversevelocity components and eddy currents that were not eliminated by otherinlet distributors. More specifically, this invention is a fluiddistributor that divides a principally axial flow of fluid into a seriesof flow passages. These flow passages end in cylindrical outlet bandshaving uniformly spaced apertures about their circumference that providea small pressure drop for circumferentially redistributing the fluidleaving each passage. The cylindrical bands of apertures areprogressively spaced at increasing distances from the inlet nozzle toincrease the dispersal of fluid flow over the entire particle bedsurface.

Accordingly, in one embodiment, this invention is a fluid distributorcomprising a conduit, a plurality of partitions, and a series ofperforations. The conduit has an inlet for receiving a fluid stream. Theplurality of partitions subdivide most of the cross-sectional area ofthe conduit into at least two annular collection zones. The partitionsalso define, at least in part, a series of outlet bands that arecentered about the longitudinal axis of the conduit. Each outlet band islocated at the end of one collection zone and the outlet bands have anarrangement wherein the outermost collection zone ends with the outletband located nearest the inlet and each successive inwardly spacedcollection zone ends with an outlet band having an increased spacingfrom the inlet. The series of perforations are spaced at regularintervals about the circumference of each band to circumferentiallyredistribute fluid flow out of each outlet band.

In another embodiment, this invention is a fluid distributor thatcomprises a cylindrical container, a plurality of partitions, andaperatures spaced uniformly about the circumference of the container.The cylindrical container has a primary inlet at one end and a closureplate at the opposite end. The plurality of partitions are located inthe container and define a series of annular inlets inside the containerand a series of cylindrical outlet bands along the wall of thecontainer. The partitions communicate each inlet with one outlet andchange the direction of fluid flow between the annular inlets and theoutlets. A portion of the apertures lie within each cylindrical outletband. The apertures are uniformly spaced circumferentially about eachoutlet band and provide a small pressure drop for circumferentiallyredistributing fluid flow out of each band.

Additional objects, embodiments, aspects, and details of this inventionare set forth in the following detailed description.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 shows an arrangement of a downflow reactor having an inletdistributor and a particle bed.

FIG. 2 is one form of the inlet distributor of this invention.

FIG. 3 is an alternate form of the inlet distributor of this invention.

FIG. 4 is a bottom view of the inlet distributor of FIG. 3.

DETAILED DESCRIPTION OF THE INVENTION

The distributor of this invention can be used in conjunction with anyparticle bed. Typically, the particle bed and inlet distributor will belocated inside a vessel for a catalytic reaction or an adsorptionprocess. This invention finds greatest advantage when used with a vesselhaving a downward flow of fluid from an inlet nozzle through anunconfined bed of particles. The invention can also be used withconfined particle beds. In confined particle beds, large scale shiftingof the upstream bed surface is not a concern due to restraint by ascreen or other confining device but disturbance of the bed surface canstill cause attrition and wear of the particles. Thus, while best suitedfor downflow type vessel, this invention can also be used in vesselswhere fluid flow is primarily horizontal or even upflow.

Most arrangements for piping fluid to the particle beds will dictate theuse of pipe bend or elbow just upstream of the inlet supplying fluidabove a particle bed surface. Passage through the bend concentratesfluid flow in the outer radius of the bend. The distributor of thisinvention is especially effective in preventing the bend effect fromcontributing to bed disturbances. Bend effects are corrected bycircumferentially redistributing the annularly segregated portions ofthe fluid flow to the particle bed.

Fluid entering the distributor of this invention may be gaseous phase,liquid phase, or a combination of the two. Greatest advantage isobtained when the fluid stream entering through the inlet distributorsis in gas phase.

This invention is more fully explained in the context of a typicaldownflow vessel arrangement as shown in FIG. 1. The remainder of thisdescription refers to the fluid as a gas. This reference is not meant tolimit the invention to gas phase flow. Referring again to FIG. 1, anupper pipe 10 delivers a gas phase fluid to a vessel 12 through an inletnozzle 14 which is connected to pipe 10 through a pipe swedge 16 and anelbow 18. If unrestricted, discharge of the fluid from elbow 18 wouldproduce a gas jet and also introduce a transverse velocity componentinto the gas stream that enters vessel 12.

However, all of the gas flow that enters vessel 12 is intercepted firstby distributor 20. Distributor 20 has an inlet plate 22 sandwichedbetween the bottom of pipe swedge 16 and the top of inlet nozzle 14.Sandwiching plate 22 between pipe swedge 16 and inlet 14 securesdistributor 20 to vessel 12 and provides a seal between pipe swedge 16and inlet plate 22 that prevents fluid from entering vessel 12 withoutfirst passing through distributor 20. Other well-known means ofattaching distributor 20 to vessel 12 or pipe swedge 16 can be used.Nevertheless, whatever method of attachment is used, it is importantthat the method prevent bypassing of fluid around distributor 20 andinto the vessel 12. This bypassing can produce concentrated jets offluid flow that will diminish or defeat the effect of distributor 20.

In a manner hereinafter described, distributor 20 disperses the gas overthe cross-section of vessel 12. The dispersed gas enters a particle bed24 having an upper surface 25. Bed 24 is composed of solid particleswhich can be in the form of pills, spheres, cylinders, or other extrudedshaped. The actual properties of the particles will depend upon theprocess which is carried out in the containment vessel. Generally,particles will consist of an adsorbent or a catalyst. As a further meansof preventing bed disturbances, a layer of support material, usuallycomprising ceramic balls, may be added and comprise the upper surface ofthe particle bed. In the case of a downflow reactor, bed surface 25 willsimply consist of particles that have been leveled at the time ofloading. In the case of a confined catalyst bed, a screen or other layerof laminar material will be at the level of surface 25. As gas passesacross upper surface 25, it proceeds down through the remainder of bed24. Once the gas has moved a short distance past the bed surface,provided the surface remains level, a complete redistribution of the gasis effected such that it will pass uniformly through the remainder ofthe bed. Therefore, it is not essential that distributor 20 provide acompletely uniform distribution of gas across the bed surface 25. Thepurpose of distributor 20 is to provide a fluid, or in this case gasdispersion, that has enough uniformity to eliminate any eddy orcross-currents having sufficient velocity to disrupt surface 25. After apredetermined contact time, gas leaves the catalyst bed 24 by passingthrough a porous support member 26. Member 26 can be screen or any otherrigid layer of porous material having sufficient strength to support theweight and pressure loading of catalyst bed 24. Exiting gases passthrough an outlet screen 28 that collects any fine particles that havepassed out of a catalyst bed and through support member 26. From screen28, exiting gases leave the vessel 12 through an outlet nozzle 30 whichis connected to a lower pipe 32.

The function of distributor 20 in dispersing fluid can be more fullyappreciated by a consideration of the device shown in FIG. 2 which isone form of a distributor designed in accordance with this invention.FIG. 2 shows inlet plate 22 having a series of perforations 34 whichcollectively provide an inlet for gas flow into the distributor.Although preferred, it is not necessary that perforations 34 be usedacross the inlet of plate 22. Inlet plate 22 may be provided with a fewlarge openings or a single opening. The use of perforations increasesthe uniformity of the gas flow into the distributor the advantage ofwhich must be balanced against an increased pressure drop across theinlet. Therefore, pressure drop considerations will control the numberand size of openings in inlet plate 22. In normal practice, the holes inthe inlet plate will be sized to provide a pressure drop at least equalto twice the velocity head of the incoming gas stream. The opening oropenings may extend as far as the wall of a conduit 36 that receives thegas flow passing through inlet plate 22. A series of partitions 42, 44,46, 48, 50, and 52 divide the projection of the cross-sectional area ofconduit 36 into a series of annular collection zones. A series of outletbands 54, 56, 58, 60, 62, and 64 are associated respectively with one ofthe partitions to define the collection zones as that volume lying inboth the space above a given partition and the cylindrical spaceconfined by each outlet band. The collection zone associated withpartition 42 and outlet 54 takes the outermost annular layer of gas flowpassing through conduit 36 and redirects it in a radial direction out ofseries of apertures 66 located in outlet band 54. Apertures 66, in thiscase, are simply a series of holes spaced circumferentially about outlet54 at a uniform spacing. The pressure drop across opening 66 is kept lowso that the horizontal velocity component created by the impact of gasflow against partition 42 will be preserved and contribute to the radialmomentum of the gas as it leaves the distributor. Holes 66 serve theimportant function of circumferentially redistributing the gas flow ateach partition. Therefore, a completely open outlet band, as practicedin the prior art, does not provide the necessary pressure drop forcircumferential redistribution. A minimum pressure drop in excess of theradial velocity head and preferably several times greater than theradial velocity head across the opening 66 will provide the necessarycircumferential redistribution. The collection zones associated with thedownstream partitions 44, 46, 48, 50, and 52 take the remaining gas flowfrom annular layers of progressively decreasing diameter and redirectsit radially outward. The gas flow deflected by each partition passesthrough apertures 66 of its respective outlet band whichcircumferentially redistribute the flow in the manner described.

Fluid that passes below partition 52 enters a final outlet arrangementwhich, in this case, consists of an outlet band 68 and a bottom plate70. End plate 70 is usually imperforate. When end plate 70 has a largediameter relative to the bed, small perforations may be provided todirect a small portion of the gas downwardly onto the center of theparticle bed to avoid the formation of a dead space below thedistributor which could again introduce eddy currents above the bed.However, the majority of the gas flow passing below partition 52 isradially redirected through outlet band 68. Any gas flow permittedthrough an opening in plate 70 should not exceed the volumetric gasaddition that satisfies the average gas flow requirements through thecentral portion of the bed that is not in the immediate flow path of theradially discharged gas. Gas flow through plate 70 can produce a jetwhich can impact and disturb the downstream bed surface. Therefore, jetlength considerations may limit the size of any opening in plate 70.

The configuration of distributor 20 will vary depending primarily on thegeometry of the vessel in which it is inserted and the number and typeof collection zones. The length of conduit 36 between inlet plate 22 andthe first outlet band is sized to get the apertures 66 below the inletnozzle 14 so that the radially directed fluid passing therethrough doesnot impinge on the nozzle wall. The number of collection zones used in aparticular distributor will vary with the velocity of gas flow, therelative size of the inlet nozzle and vessel, and the susceptibility, ofthe particle bed to flow-induced disturbance. Two or more collectionzones may be used. Generally, the more collection zones used, the betterthe distribution across the catalyst beds. In the specific configurationof the FIG. 1 distributor increasing the width of the partitions willincrease the radial gas flow at each outlet band. Adjusting the size andnumber of apertures in each outlet band will also vary the radial gasvelocity or through aperatures in different outlet bands. By appropriatesizing of the collection zones and aperatures, this distributor canprovide good gas dispersion over a particle bed of almost any shape orsize.

An alternate and often preferred arrangement for the distributor of thisinvention is shown in FIG. 3. In this case, the distributor consists ofan inlet plate 22', a cylindrical container 72, an upper partition 74,intermediate partitions 76, a lower partition 78, and an end plate 80.The upper end of container 72 referred to as the inlet or primary inletis attached to inlet plate 22'. Inlet plate 22' is perforated with aseries of equally spaced holes to provide a pressure drop for the gaspassing across the inlet plate. Partition 74 consists of an annularplate 82 which is attached along its outer perimeter to the interior ofcontainer 72 and a ring 84 which is attached to the inner perimeter ofplate 82 and extends upward towards the primary inlet. Ring 84 togetherwith the wall of cylinder 72 defines an annular inlet extending betweenthe top of ring 84 and the cylinder wall which collects gas flowtraveling in a principally downward direction along the wall of cylinder72. The gas flow is redirected radially outward by partition 74 andpasses through a series of holes 88 in an outlet band 90. Outlet band 90is defined as that section of container 72 lying in the radialprojection of ring 84. Holes 88 are again sized to provide only a smallamount of pressure drop across the outlet band.

Intermediate partitions 76 consists of annular plates 92 having theirouter perimeter attached to the inside of container 72 and an innerperimeter to which a ring 94 is attached. The number and size of holes88 in any outlet band may be adjusted to provide the desired flow rateand to some degree the desired pressure drop at any band level. Thevelocity head produced at each annular inlet provides additionalpressure drop that may be used to adjust and vary the pressure drop atany given band level without upsetting, to any great degree, the overallpressure balance across all the annular inlets. Lower partition 78consists of an annular plate 96 having its outer perimeter attached tothe inside of container 72 and an inner perimeter to which a ring 98 isattached and extends upward towards the primary inlet. Annular plates82, 92, and 96 divide the portion of container wall 72 locatedtherebetween into a number of vertically spaced outlet bands 100.Annular inlets, defined as the horizontal area between the top of onering and a superadjacent ring, collect annular sections of axiallyflowing gas from the region immediately above the annular inlets. Thegas collected by the annular inlets is redirected and discharged in aradial direction through a series of holes 88 located in annular bands100. Holes 88 are uniformly spaced about the circumference of eachoutlet band. By providing a small pressure drop, holes 88 ensure thatradial gas flow from the outlet bands is uniform across the entirecircumference. Again, only a small pressure drop through holes 88 isrequired to provide any needed circumferential redistribution. Rings 94and 98 extend upward towards the primary inlet and preferably extendsabove the next adjacent annular plate. Extending the ring above the nextadjacent annular plate defines at least a small vertical flow passagebetween adjacent rings that aids in trapping an annular section of gasflow by preventing inward deflection of the gas as it contacts thepartition and undergoes a change in direction. Preferably, the extensionof the ring above the next adjacent annular plate equals at least aquarter of the horizontal distance between the adjacent rings.

Gas flow traveling down the very center of cylindrical container 72passes inside ring 98 and into a chamber bordered by annular plate 96,plate 80, and container 72. A portion of the gas entering this chamberis directed radially outward through holes 102. The remainder of theentering gas passes downwardly through perforations in end plate 80. Thearrangement of perforations in end plate 80 is more clearly shown inFIG. 4. End plate 80 is imperforate about a central diameter equal tothe inner diameter of ring 98. The remaining area of end plate 80 isperforated by smaller holes 106 that are equally spaced about the plate.The total open area provided by holes 102 and 106 will provide a verysmall pressure drop through these openings. Small holes 106 are locatedunder annular plate 96 to prevent any direct axial gas flow out of thedistributor and preferably sized to provide a gas flow to that portionof the particle bed surface underlying horizontal projection distributorthat is at least equal to the average gas flow across the entireparticle bed surface. As previously mentioned, providing downward oraxial gas flow across the top surface of the bed prevents horizontal gasflow that could disturb the bed.

What is claimed is:
 1. A fluid distributor comprising:(a) a conduithaving an inlet for receiving a fluid stream; (b) a plurality ofpartitions subdividing at least half of the cross-sectional area of saidconduit into at least two annular collection zones said partitionshaving an inner ring that extends longitudinally toward said inlet to alevel at least equal to about the most downstream level of the precedingcollection zone; (c) a series of outlet bands spaced along and centeredabout the longitudinal axis of said conduit, with each outlet bandlocated along the outer boundary of a collection zone, said outlet bandshaving an arrangement wherein the outlet band located nearest said inletborders the outmost collection zone and succeeding outlet bands havingan increased axial spacing from said inlet border collection zones haveprogressively increasing inward locations;
 2. The distributor of claim 1wherein said conduit and said outlet bands have a uniform diameter andcomprise a cylindrical vessel having a closure plate at an end oppositesaid inlet.
 3. The distributor of claim 2 wherein said inletcommunicates with said closure plate and said closure plate isperforated.
 4. The distributor of claim 1 wherein said outlet bands haveprogressively decreasing diameters with the smallest diameter bandlocated the greatest distance from said inlet.
 5. The distributor ofclaim 1 wherein said partitions comprise annular plates having innerdiameters that progressively decrease in size as the distance of theannular plate from said inlet increases and each of said rings extendstoward said inlet from the inner diameter of each annular plate past thepreceding annular plate.
 6. The distributor of claim 1 wherein aperforated plate covers said inlet.
 7. A fluid distributorcomprising:(a) a cylindrical container having a primary inlet at one endand a closure plate at the opposite end; (b) a plurality of partitionslocated in said container and defining a series of annular inlets insidesaid container and a series of cylindrical outlet bands along the wallof said container, said partitions collectively communicating each inletwith one outlet and having an arrangement that will change the directionof any fluid flowing between said annular inlets and said outlet bandssaid partitions having an inner ring that extends longitudinally towardsaid primary inlet to a level at least equal to about the mostdownstream level of the preceding collection zone; and (c) a series ofapertures spaced uniformly about the circumference of each outlet band.8. The distributor of claim 7 wherein said aperatures are uniformlysized and spaced about said cylinder.
 9. The distributor of claim 7wherein said closure end plate contains a plurality of apertures and thefarthest partition from said primary inlet has an opening forcommunicating said primary inlet with said closure end plate.
 10. Thedistributor of claim 7 wherein said partitions comprise annular plates,each plate having its outside circumference fixed to said container andsaid inner ring is a cylindrical ring fixed to the inside circumferenceof said annular plate with each ring extending toward said primary inletand past the preceding annular plate.
 11. The distributor of claim 10wherein at least three partitions are located within said container. 12.The distributor of claim 10 wherein a perforated inlet plate covers saidprimary inlet.
 13. The distributor of claim 12 wherein said end closureplate contains a plurality of apertures and has an imperforate centralportion, said central portion having a diameter equal to or greater thanthe annular opening of the partition farthest from said primary opening.14. The distributor of claim 12 wherein the perforations in said inletplate are sized to produce a pressure drop at least equal to twice thevelocity head of any fluid entering the distributor.